EP0064608A1 - Cellule électrolytique du type filtre-presse - Google Patents

Cellule électrolytique du type filtre-presse Download PDF

Info

Publication number
EP0064608A1
EP0064608A1 EP82103143A EP82103143A EP0064608A1 EP 0064608 A1 EP0064608 A1 EP 0064608A1 EP 82103143 A EP82103143 A EP 82103143A EP 82103143 A EP82103143 A EP 82103143A EP 0064608 A1 EP0064608 A1 EP 0064608A1
Authority
EP
European Patent Office
Prior art keywords
anode
cathode
compartment
compartment frame
exchange membrane
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP82103143A
Other languages
German (de)
English (en)
Other versions
EP0064608B1 (fr
Inventor
Osamu Shiragami
Toshihiko Kuno
Yasuo Sajima
Kohji Saito
Junjiro Iwamoto
Takahiro Uchibori
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
AGC Inc
Original Assignee
Asahi Glass Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=27298154&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=EP0064608(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Priority claimed from JP56063378A external-priority patent/JPS5925035B2/ja
Priority claimed from JP56078686A external-priority patent/JPS57194286A/ja
Priority claimed from JP56166448A external-priority patent/JPS6037878B2/ja
Application filed by Asahi Glass Co Ltd filed Critical Asahi Glass Co Ltd
Publication of EP0064608A1 publication Critical patent/EP0064608A1/fr
Application granted granted Critical
Publication of EP0064608B1 publication Critical patent/EP0064608B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C25B9/77—Assemblies comprising two or more cells of the filter-press type having diaphragms
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/60—Constructional parts of cells
    • C25B9/65—Means for supplying current; Electrode connections; Electric inter-cell connections
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/70—Assemblies comprising two or more cells
    • C25B9/73—Assemblies comprising two or more cells of the filter-press type
    • C25B9/75—Assemblies comprising two or more cells of the filter-press type having bipolar electrodes

Definitions

  • the present invention relates to an electrolytic cell useful for the production of a halogen and an alkali metal hydroxide from an alkali metal halide aqueous solution or oxygen and hydrogen from an aqueous alkaline solution, and particularly to a filter press type membrane electrolytic cell.
  • Various filter press type membrane electrolytic cells are known in which a number of anodes and cathodes are alternately arranged in parallel to one another and partitioned from one another by a cation exchange membrane.
  • Electrolysis is substantially different from the case of an electrodialysis cell in that it involves an electrode reaction on the surface of an electrode and the presence of an electrode surface is thereby essential, and in the electrolysis of an alkali metal chloride aqueous solution, a chlorine gas is generated at the anode and a hydrogen gas is generated at the cathode.
  • angular hollow pipes constituting passages for an electrolytic solution and electrolized products and joined to form hollow rectangular frames defining electrode compartments, i.e. so-called hollow compartment frames.
  • the electrolytic cell having such hollow compartment frames is fairly effective and useful.
  • the compartment frames are manufactured from hollow pipes of expensive material, and accordingly, the cost of the cell becomes inevitably high involving the expensive material and manufacturing costs.
  • a so-called plate type electrolytic cell has been proposed to overcome the disadvantage of the abovementioned pipe type electrolytic cell, in which a rectangular frame gasket made of a plate is used as the compartment frame.
  • An electrolytic cell of this type is disclosed in e. g. Japanese Laid-Open Patent Application No. 108899/78, in which compartment frame gaskets made of a non-conductive flexible plate material and having a center opening constituting an electrolytic compartment, are assembled with cation exchange membranes and electrode plates to form a filter press type electrolytic cell, and the respective compartment frames, electrode plates and cation exchange membranes are provided, at their four corner portions, with holes constituting passages for the electrolytic solutions and the electrolyzed products.
  • the electrolytic cell of this type is substantially advantageous over the abovementioned cell in which hollow pipes are used.
  • it has certain drawbacks in the structures of the electrode plates and the compartment frames.
  • the electrode plates have the same size as the compartment frames, and accordingly it is necessary to provide holes not only on the compartment frames but also at the four corners of each electrode plate to constitute passages for the electrolytic solution and the electrolyzed products.
  • This brings about not only an economical disadvantage that a great amount of expensive electrode plates is required but also a fatal defect.
  • the anode plates in order to prevent electrical short circuit, it is necessary to electrically insulate the passages formed on the anode plates for the cathode solution and the cathode products from the anodes.
  • the present inventors have conducted various studies to solve the abovementioned problems, and as a result, have accomplished the present invention.
  • the present invention provides a filter press type ion exchange membrane electrolytic cell which comprises an anode compartment and a. cathode compartment partitioned by a cation exchange membrane and which is useful for obtaining a halogen, hydrogen and an alkali metal hydroxide from an alkali metal halide aqueous solution, or oxygen and hydrogen from an aqueous alkaline solution.
  • the filter press type electrolytic cell is characterized by :
  • the electrode plates have no holes at their four corner portions, and they are slightly larger than the electrode compartments to cover the latter, whereby it is possible to overcome the various disadvantages of the electrolytic cell disclosed in the abovementioned Japanese Laid-Open Patent Application.
  • an electrode plate is sandwiched between compartment frames having a rectangular center opening.
  • This electrode is prepared by providing a slit on the electrode surface and pushing the slit open to form a louver shape, and consequently, inevitably has a structure in which the flange surface is not flush with the electrode surface.
  • there is a trend for an energy- saving type electrolytic technique and an effort has been made to minimize the distance between the electrodes.
  • the electrode plate to be used in the electrolytic cell according to the present invention it is preferred to use an electrode plate in which the electrode portion is flush with the sealing portion facing the compartment frame.
  • Specific types of the electrode plate include a punched metal, an expanded metal made flat over the entire surface, and a wire mesh with its sealing portion made flat.
  • the sealing portion may be left without forming perforations, whereby liquid-tight sealing between the compartment frame and the ion exchange membrane can be facilitated.
  • the edges of the perforations of the punched metal are rounded on one side of the punched metal, and the ion exchange membrane may be disposed to face that side of the punched metaL whereby damages of the ion exchange membrane caused by the edges of the perforations can thereby be avoided.
  • the punched metal is particularly preferred as an embodiment of the electrode plate of the present invention.
  • the foraminous electrode plate is made of an expanded metal which has been made flat over the entire surface, it is possible to attach along the periphery thereof, a flat frame having substantially the same thickness as the porous electrode plate by e.g. welding so as not to form a stepped portion.
  • the expanded metal per se it is also possible to use the expanded metal per se to extend to the sealing portion, without attaching a special flange, and the portion of the expanded metal to contact the compartment frame is directly or via a packing sandwiched between the compartment frame and the ion exchange membrane.
  • an elastic material for instance, a rubber such as EPDM
  • the feature of this first embodiment resides in that the above- mentioned electrode is a porous electrode of a flat plate shape integrally formed with and being flush with the sealing portion facing the compartment frame.
  • the current input from outside to the electrode surface and the current output to outside are conducted solely by a flat foraminous electrode plate which essentially constitutes the electrode base body, whereby electrical connections to conductive ribs or conductive plates by means of welding or a bolt fastening structure, which are otherwise required at the portion where the electrode surface faces the cation exchange membrane, can be eliminated, and accordingly possible roughening of the electrode surface or formation of stepped portions which may otherwise result by such electrical connections, can be eliminated.
  • Figure 1 is a horizontally cross sectional view of a first embodiment of the electrolytic cell of the present invention comprising one cathode cell and one anode cell and illustrates a monopolar cell.
  • Foraminous anode plates 1 are a known type composed of an expanded metal made of e.g. titanium and made flat by roll pressing and ruthenium oxide coated thereon, and they are held without flanges against the respective sides of the anode compartment frame.
  • the foraminous anode plates 1 may be secured to the respective sides of the compartment frame by placing them against the sides of the frame and holding them to the frame simply by the pressure upon fastening e. g. tie rods.
  • anode compartment frame 2 is made of a resin such as polyvinyl chloride, it is desirable to place a packing between the anode plates and the anode compartment frame. However, when the anode compartment frame is made of rubber, it is unnecessary to provide such a packing between the anode plates and the frame, as shown in Figure 1.
  • the foraminous cathode plates 3 are of a low hydrogen overvoltage type which can be prepared by electro-codepositing Raney nickel particles on an expanded metal made of e.g. stainless steel and made flat by roll pressing. Like the above-mentioned anode plates, they have no flanges and are held against the respective sides of the cathode compartment frame. In the same manner as in the case of the anode plates, they can be secured to the respective sides of the cathode compartment frame by means of securing hooks. However, in the embodiment illustrated in Figure 1, they are simply held against the sides of the frame without such hooks.
  • the cathode compartment frame is made of a resilient material, it is unnecessary to provide a packing between the cathode plates and the cathode compartment frame, as shown in Figure 1. However, if a material having no or little resiliency such as a polyvinyl chloride resin is used for the cathode compartment frame, it is desirable to use a packing.
  • the cation exchange membrane 5 are made of a sheet of e. g. perfluorocarbon having carboxylic acid groups as ion exchange groups and having a thickness of from 100 to 300pm, and they are suitable particularly for alkali metal chloride electrolysis or water electrolysis.
  • the cation exchange membrane 5 is sandwiched between the foraminous anode plate 1 and the foraminous cathode plate 3 and held at the anode compartment frame and the cathode compartment frame.
  • the cation exchange membrane 5 is thin and lacks in adequate resiliency and it is preferred to provide packings 6 and 7 between the cation exchange membrane and the foraminous anode plate and between the cation exchange membrane and the foraminous cathode plate, at the respective frame portions.
  • only one packing & or 7 may suffice.
  • the foraminous anode plate and cathode plate are respectively provided with projections to which anode connecting plates 8 and cathode connecting plates 9 are respectively welded.
  • the connecting plates 8 and 9 are connected to an anode bus bar 11 and a cathode bus bar (not shpwn), respectively.
  • the manner of the connection to the bus bar is illustrated in Figure 1 only with respect to the anode side, in which flexible connecting plates 10 are connected to the anode connecting plates 8 and the anode bus bar 11 is connected to the flexible connecting plates 10.
  • the connection between the electrolytic cell and the bus bar can be made flexible.
  • it is preferred that the same arrangement is employed for the cathode side as well.
  • an anode support 12 having a thickness slightly thicker than the thickness of the anode frame is inserted in the anode compartment to deflect the porous anode plates toward the porous cathode plates so that the distance between the anode and the cathode is thereby minimized or preferably the anode and cathode are brought into contact with the cation exchange membrane.
  • the anode support 12 illustrated in Figure 1 is a pipe. However, it may be a resilient member such as a spring or a leaf spring-.
  • a desired number of cell units each comprising the porous anode plates, the porous cathode plates, the cation exchange membranes, the anode frame and the cathode frame, are repeatedly arranged and an anode side plate and a cathode side plate are disposed at their respective ends, and they are fastened by tie rods to form a filter press type electrolytic cell of the present invention.
  • the electrolytic cell thus assembled is free from leakage at the fastening portions inspite of the fact that porous electrode plates having no flanges are employed. Thus, the electrolytic cell can readily be manufactured.
  • Figure 2 is a plan view showing disassembled various parts of the electrolytic cell of Figure 1 with the cation exchange membrane and the packing omitted.
  • the compartment frame 2 or 4 has four holes which constitute passages for the electrolytic solutions and the electrolyzed products.
  • the four holes constitute passages for the anode electrolytic solution, the electrolyzed product of the anode side, a cathode electrolytic solution and the electrolyzed product of the cathode side.
  • the passage for the anode electrolytic solution and the passage for the anode side electrolyzed product are respectively in communication with the anode compartment 15 having a hollow structure via communicating holes (not shown).
  • the passage for the cathode electrolytic solution and the passage for the cathode side electrolyzed product are respectively in communication with the cathode compartment 16 having a hollow structure via communicating holes (not shown).
  • the electrolytic cell is a monopolar cell
  • the same construction is applicable also to a bipolar cell.
  • the central opening of the compartment frame is divided by a partition into two compartments or chambers, and a foraminous anode plate is placed on one side of the compartment frame and a foraminous cathode plate is placed on the other side of the compartment frame so that the portion defined by the foraminous anode plate and the partition constitutes an anode compartment and the portion defined by the foraminous cathode plate and the partition constitutes a. cathode chamber.
  • the partition may be made of a conductive material such as a known bimetal, which may then be electrically connected to the foraminous anode plate and the foraminous cathode plate. Otherwise, the partition may be made of a non-conductive material, and the foraminous anode plate and the foraminous cathode plate provided in the abovementioned manner may then be made to protrude, out of the electrolytic cell for electrical connection.
  • Figure 3 is a perspective view illustrating various parts of the second embodiment of the electrolytic cell of the present invention, in which an electrode compartment frame is provided on each side of the cation exchange membrane.
  • Cathode compartment frames 18 and 20 and anode compartment frames 22 and 24 are preferably made of a non-conductive elastic material such as natural rubber or synthetic rubber.
  • One of the cathode compartment frames i.e. the frame 20 in the illustrated embodiment
  • one of the anode compartment frames i.e. the frame 24 in the illustrated embodiment
  • the cathode compartment frames 18 and 20 and the anode compartment frames 22 and -24 may be made of a resin having little elastisity. In this case, it is desirable to insert a thin gasket between the frame and the electrode conductive plate.
  • Each of the cathode compartment frames and anode compartment frames has an opening at its center and four holes having different functions in the vicinity of its corners-, and the abovementioned cation exchange membrane 21 likewise has four holes having different functions.
  • the opening 27 of the cathode frame constitutes a cathode compartment
  • the opening 27' of the anode compartment frame constitutes a anode compartment
  • the holes 28, 28' and 28" provided on the cation exchange membranes, the cathode compartment frames and the anode compartment frames, respectively, constitute a passage for a alkali metal hydroxide aqueous solution and a hydrogen gas.
  • the holes 30, 30' and 30" (30' and 30" are not shown) provided on the cation exchange membranes, the cathode compartment frames and the anode compartment frames, respectively, constitute a passage for an electrolytic brine or an electrolytic alkali metal hydroxide aqueous solution (in the case of water electrolysis).
  • the holes 31, 31' and 31" provided on the cation exchange membrane, the cathode compartment frames and the anode compartment frames, respectively constitute a passage for water or a dilute alkali metal hydroxide aqueous solution. These holes are so located that when these parts are assembled to form a filter press type electrolytic cell, the respective holes coincide to form the respective passages.
  • the cathode compartment frames 18 and 20 are provided with fluid pathway slits or through-holes 32 and 32', respectively, which connect the hole 28' to the opening 27, and the hole 31' to the opening 27, respectively,. so that a liquid and gas can flow therethrough.
  • the anode compartment frames 22 and 24 are provided with fluid pathway slits or through holes 33 and 33' (33' is not shown), respectively, which connect the hole 29" to the opening 27' and the hole 30" (not shown) to the opening 27', respectively, so that a liquid and gas can flow therethrough.
  • an electrolytic brine or an electrolytic alkali metal hyroxide aqueous solution flowing through the passage formed by the holes 30, 30' and 30" (30' and 30" are not shown) is introduced into the anode compartment 27' via the fluid pathway slit 33',. and a depleted brine and a halogen gas after the electrolysis, or an alkali metal hydroxide solution and an oxygen gas after the electrolysis are withdrawn via the fluid pathway slit 33 to the passage formed by the holes 29, 29' and 29".
  • water or an alkali metal hydroxide solution flowing through the passage formed by the holes 31, 31' and 31" is introduced into the cathode compartment 27 via the fluid pathway slit 32', and an alkali metal hydroxide aqueous solution and hydrogen after the electrolysis are withdrawn ⁇ via the fluid pathway slit 33 to the passage formed by the holes 28, 28' and 28".
  • One of the features of the second embodiment resides in the structure where the electrode plate is fit in the electrode compartment frame. Namely, a conductive plate smaller than the electrode compartment frame and slightly larger the electrode compartment is set on the electrode compartment frame to cover the electrode compartment, and another electrode compartment frame or the cation exchange membrane is placed against the other side of the conductive plate and tightened to form a filter press type assembly, whereby the following advantages are obtainable.
  • the conductive plate had the same size as a gasket, it would be required to provide holes thereon corresponding to the holes 28, 29, 30 and 31, and consequently the conductive plate would be electrically connected to the fluid flowing through the holes, as mentioned above.
  • the conductive plate is fit in the electrode compartment frame preferably in such a manner that on one side of the electrode compartment frame, a recess having a size and depth corresponding to the size and the thickness of the condutive plate is provided along the inner periphery forming the opening constituting the electrode compartment, whereby the conductive plate can be set on the recess with its surface being flush with the surface of the electrode compartment frame without being protruded therefrom, and thus the fluid leakage can thereby be avoided.
  • the basic materials and active ingredients may be those which will be described hereinafter, and as their structure, the following has been found particularly preferred.
  • At least two projections are formed, by e.g. press forming, on a center portion of the condutive plate along its longitudinal direction, and an electrode. plate is electrically and mechanically connected to the tops of the projections., whereby the cation exchange membrane can be brought in contact with or intimately fit on the anode 36 and the cathode 35, or the anode 36 and the cathode 35 can be brought to engage with each other with the cation exchange membrane inbetween.
  • the cathode plate 19 is fit in the recess 34 formed on the cathode compartment frame 20 and having the same configuration (i.e. the same size and thickness) as the cathode conductive plate 19, while the anode condutvive plate 23 is fit in the recess 34' formed on the anode compartment frame 24 and having the same configuration (i.e. the same size and thickness) as the anode condutive plate 23.
  • Figure 4 illustrates an example of a preferred construction of the conductive plate and the electrode to be used for the electrolytic cell of Figure 3.
  • the electrode 35 or 36 slightly smaller than the condutive plate 19 or 23 is electrically connected to the conductive plate 19 or 23.
  • a conductive bus bar 25 or 26 for supplying electric current to the conductive plate 19 or 23 is electrically and mechanically connected to the conductive plate.
  • Figure 5 is a cross section taken along the line A-A of Figure 4.
  • Figure 5 illustrates a preferred construction of the conductive plate and the electrode to be used for the electrolytic cell of Figure 3.
  • the configurations of the projections along the longitudinal direction of the conductive plate 19 or 23 are not limited to the particular configurations illustrated, and they may be in a semi-circular or semi-oval shape or in a form of plate-shaped ribs, etc.
  • the electrode 35 or 36 is electrically and mechanically connected to the tops of the projections of the condutive plate 19 or 23 to form a flat configuration. Further, the ends of the electrode 35 or 36 are preferably bent toward the conductive plate to avoid the rupture of the cation exchange membrane.
  • the electrodes 35 and 36 are selected to have elastisity. It is preferred to use an expanded metal having a major length of from 3 to 20 mm, a minor length of from 1.5 to 10 mm, and a strand width of from 0.2 to 2 mm. Further, the height of the projections is preferably from 3 to 30 mm. The thickness of the conductive plate is preferably from 0.5 to 5 mm.
  • Figure 6 illustrates an embodiment wherein the anode 36 and the cathode 35 are assembled to engage with each other.
  • the projections of the cathode conductive plate 19 are located at intermediate positions between the projections of the anode conductive plate 23.
  • the height of the projections relative to the thickness of the electrode compartment frames are adjusted so that when the electrode compartment frames are tightened,-the anode and the cathode will be brought to engage with each other.
  • the anode 36 and the cathode 35 can be brought to engage with each other.
  • the degree of the engagement of the anode and the cathode is to such an extent that the anode 36 and the cathode 35 are thereby brought in contact with or intimately fit on the cation exchange membrane 17, and it is usually from 0 to 3 mm. If the degree of the engagement exceeds 3 mm, the cation exchange membrane will be pressed excessively thus leading to the rupture of the cation exchange membrane.
  • the electrolytic cell of the second embodiment is simple in structure, superior in efficiency and economical. Another feature of this embodiment is that the weight of the electrolytic cell is substantially lighter than the conventional electrolytic cells, whereby the assembling and transportation operations can readily be done.
  • the electrolytic cell of this embodiment is assembled by putting a number of repeating units together, each unit consisting of the combination. of Figure 3, and tightening them by tie rods with rigid fastening members placed at their both ends.
  • the fastening members are required to have a substantial weight, but even with such fastening members, it is possible to reduce the overall weight of the assembled electrolytic cell..
  • a polymer containing cation exchange groups such as carboxylic acid groups, sulfonic acid groups, phosphoric acid groups or phenolic hydroxyl groups.
  • a fluorine-containing polymer is particularly preferably used.
  • Suitable fluorine-containing polymers having ion exchange groups include copolymers of a vinyl monomer such as tetrafluoroethylene and chlorotrifluoroethylene with a perfluorovinyl monomer having ion-exchange groups such as sulfonic acid groups, carboxylic acid groups or phosphoric acid groups, or reactive groups which can be converted to such ion exchange groups.
  • a membrane of a polymer of trifluorostyrene to which ion exchange groups such as sulfonic acid groups are introduced, or a polymer of styrenedivinylbenzene to which sulfonic acid groups are introduced.
  • the current efficiency as high as at least 90% is obtainable even when the sodium hydroxide concentration is at least 40%.
  • the carboxylic acid group content per gram of the abovementioned dried resin is from 1.12 to 1.7 miliequivalence, whereby highly concentrated sodium hydroxide as mentioned above can continuously be obtained with high current efficiency for a long period of time.
  • the ion exchange group content is from 0.5 to 2.5 miliequivalence, preferably from 1.12 to 2.0 miliequivalence.
  • the cation exchange membrane to be used in the present invention may be formed by blending an olefin polymer such as polyethylene or polypropylene, preferably a fluorine-containing polymer such as polytetrafluoroethylene or a copolymer of ethylene and tetrafluoroethylene, at the time of the membrane formation, as the case requires. Otherwise, it is also possible to reinforce the membrane by using a support such as a cloth, a woven fabric such as a net or a non-woven fabric which is made of such a polymer, or wires, a net or a perforated plate made of metal.
  • an olefin polymer such as polyethylene or polypropylene
  • a fluorine-containing polymer such as polytetrafluoroethylene or a copolymer of ethylene and tetrafluoroethylene
  • the cation exchange membrane as mentioned above may be used per se. However, it is preferred to use the following type of a cation exchange membrane, whereby the cell voltage can further be reduced.
  • a gas and liquid permeable non-electrode porous layer is formed on the surface of the cation exchange membrane, and the anode or the cathode is arranged via such a layer.
  • the electrodes are arranged via the abovementioned gas and liquid permeable porous layers, and they do not directly contact the membranes. Accordingly, the anodes are not required to have great alkaline resistance, and conventional electrodes having chlorine-resistance can be used. Further, the electrodes may not be bonded to the membranes or the porous layers, and thus their life is independent from the life of the membranes, i.e. they do not become useless depending upon the life of the membranes.
  • the cell voltage becomes unexpectedly low, and remarkably lower than the case where an alkali metal chloride is electrolyzed in an electrolytic cell in which the anodes and cathodes are in direct contact with the cation exchange membranes without interposition of the abovementioned porous layers.
  • the electrodes are intimately contacted with the membranes as disclosed in Japanese Laid-Open Patent Application No. 112398/79, such a low cell voltage is attainable even when the abovementioned porous layer is formed by a layer of substantially non-conductive non-electrode particles, and thus this should be regarded as a totally unexpected effect.
  • the gas and liquid permeable and corrosion resistant porous layer is inactive as an anode or cathode. Namely, it is made of a material such as a non-conductive material having greater oxygen overvoltage or hydrogen overvoltage than the electrode disposed via the porous layer.
  • a material there may be mentioned a single substance or a mixture of oxides, nitrides, carbides of such elements as titanium, zirconium, niobium, tantalum, vanadium, manganese, molybdenum, tin, antimony, tungsten, bismuth, indium, cobalt, nickel, beryllium, aluminum, chromium, iron, potassium, germanium, selenium, yttrium, silver, lanthanum, cerium, hafnium, lead, thorium, and rare earth elements.
  • oxides such elements as titanium, zirconium, niobium, tantalum, vanadium, manganese, molybdenum, tin, antimony, tungsten, bismuth, indium, cobalt, nickel, beryllium, aluminum, chromium, iron, potassium, germanium, selenium, yttrium, silver, lanthanum, cerium, hafnium, lead, thorium
  • the material for the anode side preferred is a single substance or a mixture of oxides, nitrides or carbides of such elements as titanium, zirconium, niobium, tantalum, vanadium, manganese, molybdenum, tin, antimony, tungsten and bismuth.
  • the material for the cathode side preferred is a single substance or a mixture of oxides, nitrides or carbides of such elements as titanium, zirconium, niobium, tantalum, indium, tin, manganese, cobalt and nickel.
  • a porous layer of the present invention is formed by such a material
  • the material is used in a form of powder or particles preferably in combination with a suspension of a fluorine-containing polymer such as polytetrafluoroethylene.
  • a surfactant may be used to obtain a homogeneous mixture of the two components.
  • the mixture is applied to the ion exchange membrane to form a layer thereon, and pressure of heat is applied to the ion exchange membrane to bond or preferably partially embed the layer to the membrane.
  • porous layers may be substantially the same for the anode and cathode sides, and it is suitable that they have an average pore size of from 0.01 to 2000p, a porosity of from 10 to 99%, and an air permeability of from 1 ⁇ 10 -5 to 10 moles/cm 2 .mm.cm Hg.
  • the desired low cell voltage can not be attained or the reduction of the cell voltage becomes unstable.
  • Particularly preferred ranges of the properties are such that the average pore size is from 0.1 to 1000 ⁇ , the porosity is from 20 to 98% and the air permeability is from 1 x 10 -4 to 1 mole/cm 2 .mm.cm Hg, whereby the electrolytic operation can be carried out constantly at a stabilized low cell voltage.
  • the thickness of the porous layer may be determined depending upon the nature and physical properties of the material to be used, and it should not be less than the thickness of the cation exchange membrane on which the layer is formed, and is usually from 0.1 to 500 ⁇ , preferably from 1 to 300 ⁇ .
  • the thickness is not in the abovementioned range, it is likely that the- electric. resistance becomes high, the removal of gas becomes difficult or the transfer of the electrolytic solution becomes difficult.
  • the electrode may preferably be brought in contact with the porous layer. It is possible to provide an electrode, i.e. an anode or cathode, on only one side of the ion exchange membrane. However, it is preferred to provide an electrode on each of the anode and. cathode sides of the ion exchange membrane, so as to attain better reduction of the electrolytic cell voltage.
  • the procedure may be such that a powder to form the porous layer is applied to the ion exchange membrane by e.g. screen printing and then heat pressed to form a porous layer on the surface of the ion exchange membrane, and the electrode is pressed against the surface of the porous layer.
  • the electrode compartment frames of the present invention there may be used those disclosed in Japanese Laid-Open Patent Application No. 108899/78. Namely, they may be readily manufactured by providing an opening for constituting an electrode compartment at a center portion of a plate made of a non-conductive flexible material such as a polyvinyl chloride resin or a non-conductive flexible and elastic material such as natural rubber or synthetic rubber such as EPDM, and holes smaller than the opening at the four corners of the plate to constitute passages for the electrolytic solution, and the electrolyzed products.
  • a non-conductive flexible material such as a polyvinyl chloride resin or a non-conductive flexible and elastic material such as natural rubber or synthetic rubber such as EPDM
  • the cell voltage can further be reduced in a case where the ratio of the height of the electrode compartment to the thickness of the compartment frame falls within a certain specific range.
  • the above effectiveness is obtainable when the said ratio is preferably from 20 to 500, more preferably from 30 to 350.
  • a conventional electrolytic cell in which a cation exchange membrane is used it used to be a decisive factor influencing the cell voltage that how quickly the gas generated at the electrode can be withdrawn from the electrode compartment, and it used to be impossible to substantially minimize the thickness of the compartment frame (i.e. in the case a spacer is used, the thickness of the compartment frame includes the thickness of the spacer) relative to the height of the electrode compartment, whereby a filter press electrolytic cell thereby obtainable tended to be long relative to the number of cells used.
  • the said ratio used to be at most about 30.
  • the sizes of the cathode compartment frames and the anode compartment frames vary depending upon the production capacity of the particular electrolytic cell.
  • the said thickness is from 3 to 50 mm and the said height is from 250 to 5000 mm
  • the ratio of the height to the thickness may be selected to fall within a range of from 20 to 500.
  • the electrode is a foraminous electrode made of a perforated material such as an expanded metal, a punched metal or wire meshes and being a gas and liquid permeable type.
  • the anode may be the one prepared by coating the abovementioned perforated electrode base material with a known electrode active component, for instance, a platinum group metal such as platinum, palladium, rhodium or ruthernium; an alloy thereof; or an oxide of a platinum group metal or an alloy of a platinum group metal.
  • the cathode may be a foraminous electrode made of metal such as iron, stainless steel or nickel.
  • the cathode is preferably the one obtained by subjecting stainless steel to etching treatment as disclosed in Japanese Laid-Open Patent Application No. 102279/78, or the one electrolplated with developed or undeveloped Raney alloy particles. Now, the invention will be described in more detail with reference to Examples.
  • Compartment frames made of EPDM and having a size of 1400 mm x 260 mm x 10 mm were prepared which had a center opening (i.e. electrode compartment) of 1000 mm x 200 mm and four corner holes. Out of the four holes, two holes located at the upper portions and a size of 150 mm x 90 mm, and two holes located at the lower portions had a size of 70 mm x 70 mm.
  • Foraminous anode plates having a size of .1060 mm x 290 mm were prepared which were obtained by coating ruthenium oxide on an expanded metal made of titanium, made flat by roll pressing and having perforations with a major length of 8 mm and a minor length of 4 mm and a thickness of 1.0 mm.
  • foraminous cathode plates having a size of 1060 mm x 290 mm were prepared which were obtained by electroplating Raney nickel on an expanded metal made of nickel, made flat by roll pressing and having perforations with a major length of 8 mm and a minor length of 4 mm and a thickness of 0. 8 mm.
  • an anode-connecting plate made of titanium and having a size of 1000 mm x 40 mm and a cathode-connecting plate made of nickel and having a size of 1000 mm x 40 mm were respectively attached by welding, to which an anode side flexible connecting plate and a cathode side flexible connecting plate were respectively attached.
  • each anode compartment frame Along the peripheral portion of each anode compartment frame, anode plate-securing holes were provided, and anode-securing hooks were provided on each porous anode plate at positions corresponding to the. securing-holes.
  • An anode bus bar was bolted to each anode side flexible connecting plate, and a cathode bus bar was bolted to each cathode side flexible connecting plate.
  • a titanium pipe having an outer diameter of 12 mm and a length of 700 mm was inserted in the center portion of each anode compartment to slightly outwardly deflect each porous anode plate so that the anode plate and the adjacent cathode plate were brought in contact with the cation exchange membrane.
  • sodium chloride electrolysis was conducted at 20 A/dm at 90°C.
  • the sodium hydroxide aqueous solution thereby formed had a concentration of 35%, the chlorine gas had a purity of 97.4% and the current efficiency in the cathode side was 94.4%.
  • the electrolysis was continued for 60 days. During the period, the cell voltage remained at a level of 2.96V and no liquid leakage was observed.
  • Example 2 In the same manner as in Example 1, a bipolar electrolytic cell was assembled except that a partition of a tetrafluoroethylene resin having a size of 1060 mm x 260 mm x 10 mm was provided in the center opening of each compartment frame similar to the one used in Example 1 except for the thickness being 2.0 mm, the porous anode plate was provided on one side of the compartment frame and the porous cathode plate was provided on the other side of the compartment frame, a titanium anode support having an outer diameter of 7 mm and a length of 700 mm was inserted between the partition and the porous anode plate, and both electrodes were electrically connected outside of the electrolytic cell.
  • a partition of a tetrafluoroethylene resin having a size of 1060 mm x 260 mm x 10 mm was provided in the center opening of each compartment frame similar to the one used in Example 1 except for the thickness being 2.0 mm
  • the porous anode plate was provided on one side of the compartment frame and
  • an anode conductive plate was used instead of the anode end plate, and it was connected to a positive power source
  • a cathode conductive plate was used instead of the cathode end plate, and it was connected to a negative power source.
  • the electrolytic conditions were the same as in Example 1.
  • the electrolytic performance was as follows:
  • Example 1 The operation was conducted in the same manner as in Example 1 except that the electrode plates, the thickness of the cation exchange membranes and the current density in Example 1 were changed as follows:
  • Electrode plates Porous anode plates were prepared from a titanium plate having a size of 1060 mm x 290 mm x 1 mm (thickness) by punching it out to form rhombic perforations having a major length of 8.0 mm and a minor length of 4.0 mm and with a strand width of 1. 2 mm, within an area of 1000 mm x 200 mm at the center portion of the plate, and coating it with ruthenium oxide. Porous cathode plates were prepared by electroplating Raney nickel particles on an iron base plate having the same shape as the abovementioned anode plate in an amount of 3 g/dm 2 .
  • the thickness of the cation exchange membranes 140 ⁇ .
  • the current density 30 A/dm .
  • the cell voltage was 3.03 V and the current efficiency was 93.5%, and these values remained unchanged during the electrolysis for 60 days. During the period, no liquid leakage was observed.
  • An electrolytic cell as shown in Figure 3 was assembled in which a height and a width of an anode compartment and a cathode compartment are 1000 mm and 200 mm, respectively and in which the thickness of the anode compartment frames and the cathode compartment frames was 7 mm (the ratio of the height to the thickness being 143).
  • An anode conductive plate as shown in Figure 5 was prepared from a titanium plate having a thickness of 1 mm by forming projections having a height of 7 mm, and an anode made of a titanium expanded metal having a major length of 6 mm, a minor length of 3 mm and a thickness of 0.5 mm and coated with palladium oxide was attached on the tops of the projections of the anode conductive plate by electric resistance welding.
  • a cathode conductive plate as shown in Figure 5 was prepared from an iron plate having a thickness of 1 mm by forming projections having a height of 3.5 mm, and a cathode made of an iron expanded metal having a major length of 6 mm, a minor length of 3 mm and a thickness of 0.5 mm and electroplated with Raney nickel was attached to the tops of the projections of the cathode conductive plate by electric resistance welding.
  • tin oxide powder having a particle size of at most 44 11 was suspended in 50 cc of water, and a polytetrafluoroethylene (PTFE) suspension (Tradename: Teflon 30J, manufactured by DuPont Co.) was added thereto so that the amount of PTFE became 7.3 mg.
  • PTFE polytetrafluoroethylene
  • a drop of a non-ionic surfactant (Tradename: Tritone X-100, manufactured by Rohm & Haas Co.) was added thereto, and the mixture was stirred by a supersonic stirrer under cooling with ice, and then vacuum-filtered on a porous PTFE membrane, whereupon a porous tin oxide thin layer was obtained.
  • This thin layer had a thickness of 30 ⁇ , a porosity of 73% and an air permeability of 3.8 x 10 -3 mole/cm 2 .min.cmHg and contained 5 mg/ cm of tin oxide.
  • the size of this cation exchange membrane having the porous layers was 1060 mm in height and 260 mm in width and thus was large enough to cover the electrode compartment.
  • the anode compartment frames and the cathode compartment frames were made of synthetic rubber, and the holes provided thereon corresponding to the holes 30 and 31 of Figure 3 had a size of 70 x 70 mm and the holes corresponding to the holes 28- and 29 had a size of 70 x 150 mm.
  • an electrolytic cell comprising two anode conductive plates attached with anodes and three cathode conductive plates attached with cathodes was assembled so that the degree of the engagement of the anodes with the cathodes became about 1 mm.
  • a total of 1.6 KA of electric current was conducted.
  • An apparent current density was 20 A/dm 2 .
  • the cell voltage was 2. 96 V.
  • titanium oxide powder having a particle size of at most 25 ⁇ were mixed, and after adequately mixing them, 2 parts of isopropyl alcohol and 1 part of cyclohexanol were added. The mixture was again kneaded, whereupon a paste was obtained.
  • the printed layer formed on the ion exchange membrane was dried in the air and the paste was thereby solidified.
  • titanium oxide having a particle size of at most 25p was screen printed on the other side of the ion exchange membrane.
  • the printed layers were press-fixed on the ion exchange membrane at a temperature of 140°C and under pressure of 30 kg/cm 2 and then immersed in an aqueous solution of 25% by weight of potassium hydroxide at 90°C to hydrolyze the ion exchange membrane and to elute the methyl cellulose.
  • the titanium oxide layer thus formed on the ion exchange membrane had a thickness of 20 ⁇ and a porosity of 70% and contained 1.5 mg/cm 2 of titanium oxide.
  • an expanded metal of nickel (a minor length of 2.5 mm and a major length of 5.0 mm) at the anode side of the ion exchange membrane and an expanded metal of SUS 304 (a minor length of 2.5 mm and a major length of 5.0 mm) at the cathode side, were subjected to etching treatment in a 52% sodium hydroxide aqueous solution at 150°C for 52 hours, and the cathode thus treated to have a low hydrogen overvoltage was pressed against the ion exchange membrane under pressure of 0.01 kg/cm 2 , While supplying a 30% potassium hydroxide aqueous solution to the anode compartments and water to the cathode compartments, and maintaining the potassium hydroxide concentration in the anode and cathode compartments at a level of 20%, the electrolysis was conducted at 100°C, whereupon the following results were obtained.
  • the electrolysis was conducted in the same manner as in Example 4 except that the height and the thickness of the cathode compartment frames and the anode compartment frames and the height of the electrodes and the cation exchange membranes provided with a non-electrode porous layer, were changed as shown in Table 1. The results: thereby obtained are also shown in Table 1.
  • the electrolytic performance thereby obtained was such that the cell voltage was 3.41 V and the current efficiency was 91%.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
EP82103143A 1981-04-28 1982-04-14 Cellule électrolytique du type filtre-presse Expired EP0064608B1 (fr)

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
JP56063378A JPS5925035B2 (ja) 1981-04-28 1981-04-28 フイルタ−プレス式電解槽
JP63378/81 1981-04-28
JP78686/81 1981-05-26
JP56078686A JPS57194286A (en) 1981-05-26 1981-05-26 Filter press type electrolytic cell
JP56166448A JPS6037878B2 (ja) 1981-10-20 1981-10-20 イオン交換膜電解槽
JP166448/81 1981-10-20

Publications (2)

Publication Number Publication Date
EP0064608A1 true EP0064608A1 (fr) 1982-11-17
EP0064608B1 EP0064608B1 (fr) 1987-09-16

Family

ID=27298154

Family Applications (1)

Application Number Title Priority Date Filing Date
EP82103143A Expired EP0064608B1 (fr) 1981-04-28 1982-04-14 Cellule électrolytique du type filtre-presse

Country Status (6)

Country Link
US (1) US4605482A (fr)
EP (1) EP0064608B1 (fr)
AU (1) AU551125B2 (fr)
BR (1) BR8202421A (fr)
CA (1) CA1203507A (fr)
DE (1) DE3277310D1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0220846A1 (fr) * 1985-10-22 1987-05-06 Imperial Chemical Industries Plc Cellule électrolytique
EP0145259B1 (fr) * 1983-11-14 1988-10-19 Imperial Chemical Industries Plc Procédé pour l'électrolyse d'une solution aqueuse d'un chlorure de métal alcalin
EP0443430A1 (fr) * 1990-02-15 1991-08-28 Asahi Glass Company Ltd. Assemblage de cellules électrolytiques monopolaires à membrane échangeuse d'ions
US5254233A (en) * 1990-02-15 1993-10-19 Asahi Glass Company Ltd. Monopolar ion exchange membrane electrolytic cell assembly
WO2022241518A1 (fr) * 2021-05-19 2022-11-24 Plastic Fabricators (WA) Pty Ltd t/a PFWA Cellule d'électrodialyse

Families Citing this family (46)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4755272A (en) * 1986-05-02 1988-07-05 The Dow Chemical Company Bipolar electrochemical cell having novel means for electrically connecting anode and cathode of adjacent cell units
FR2601387B1 (fr) * 1986-07-09 1990-10-19 Solvay Electrolyseur du type filtre-presse
WO1996019839A1 (fr) * 1994-12-19 1996-06-27 Motorola Inc. Materiaux pour electrodes et dispositifs electrochimiques dotes de ces derniers
US6132572A (en) * 1998-09-17 2000-10-17 Kyungwon Enterprise Co., Ltd. Apparatus and method of producing water for deodorization and cleaning applications
US6919010B1 (en) 2001-06-28 2005-07-19 Novellus Systems, Inc. Uniform electroplating of thin metal seeded wafers using rotationally asymmetric variable anode correction
US6254741B1 (en) * 1999-08-05 2001-07-03 Stuart Energy Systems Corporation Electrolytic cells of improved fluid sealability
US8475636B2 (en) 2008-11-07 2013-07-02 Novellus Systems, Inc. Method and apparatus for electroplating
US8308931B2 (en) * 2006-08-16 2012-11-13 Novellus Systems, Inc. Method and apparatus for electroplating
US7622024B1 (en) 2000-05-10 2009-11-24 Novellus Systems, Inc. High resistance ionic current source
US6821407B1 (en) 2000-05-10 2004-11-23 Novellus Systems, Inc. Anode and anode chamber for copper electroplating
US6527920B1 (en) 2000-05-10 2003-03-04 Novellus Systems, Inc. Copper electroplating apparatus
US7682498B1 (en) 2001-06-28 2010-03-23 Novellus Systems, Inc. Rotationally asymmetric variable electrode correction
EP1528126A1 (fr) * 2003-10-30 2005-05-04 Vandenborre Hydrogen Systems N.V. Module d'électrolyseur intégré avec separateur gaz/liquide
US8623193B1 (en) 2004-06-16 2014-01-07 Novellus Systems, Inc. Method of electroplating using a high resistance ionic current source
WO2006060912A1 (fr) * 2004-12-07 2006-06-15 Stuart Energy Systems Corporation Electrolyseur et composants les contenant.
US7494583B2 (en) * 2005-06-29 2009-02-24 Oleh Weres Electrode with surface comprising oxides of titanium and bismuth and water purification process using this electrode
RU2427669C2 (ru) * 2006-09-29 2011-08-27 Уденора С.П.А. Электролитическая ячейка
US7799684B1 (en) 2007-03-05 2010-09-21 Novellus Systems, Inc. Two step process for uniform across wafer deposition and void free filling on ruthenium coated wafers
US8513124B1 (en) 2008-03-06 2013-08-20 Novellus Systems, Inc. Copper electroplating process for uniform across wafer deposition and void free filling on semi-noble metal coated wafers
US8703615B1 (en) 2008-03-06 2014-04-22 Novellus Systems, Inc. Copper electroplating process for uniform across wafer deposition and void free filling on ruthenium coated wafers
US7964506B1 (en) 2008-03-06 2011-06-21 Novellus Systems, Inc. Two step copper electroplating process with anneal for uniform across wafer deposition and void free filling on ruthenium coated wafers
US20120261254A1 (en) 2011-04-15 2012-10-18 Reid Jonathan D Method and apparatus for filling interconnect structures
US8475637B2 (en) * 2008-12-17 2013-07-02 Novellus Systems, Inc. Electroplating apparatus with vented electrolyte manifold
US8262871B1 (en) 2008-12-19 2012-09-11 Novellus Systems, Inc. Plating method and apparatus with multiple internally irrigated chambers
US9624592B2 (en) 2010-07-02 2017-04-18 Novellus Systems, Inc. Cross flow manifold for electroplating apparatus
US8795480B2 (en) 2010-07-02 2014-08-05 Novellus Systems, Inc. Control of electrolyte hydrodynamics for efficient mass transfer during electroplating
US10094034B2 (en) 2015-08-28 2018-10-09 Lam Research Corporation Edge flow element for electroplating apparatus
US10233556B2 (en) 2010-07-02 2019-03-19 Lam Research Corporation Dynamic modulation of cross flow manifold during electroplating
US9523155B2 (en) 2012-12-12 2016-12-20 Novellus Systems, Inc. Enhancement of electrolyte hydrodynamics for efficient mass transfer during electroplating
CN103114299A (zh) * 2013-02-08 2013-05-22 大连交通大学 由硼砂制取硼酸的电解装置及方法
US9670588B2 (en) 2013-05-01 2017-06-06 Lam Research Corporation Anisotropic high resistance ionic current source (AHRICS)
US9449808B2 (en) 2013-05-29 2016-09-20 Novellus Systems, Inc. Apparatus for advanced packaging applications
US9677190B2 (en) 2013-11-01 2017-06-13 Lam Research Corporation Membrane design for reducing defects in electroplating systems
EP3095896B1 (fr) * 2014-01-15 2020-04-01 Thyssenkrupp Uhde Chlorine Engineers (Japan) Ltd. Anode pour réacteur d'électrolyse à membrane échangeuse d'ions, et réacteur d'électrolyse à membrane échangeuse d'ions utilisant celle-ci
CN103938413B (zh) * 2014-04-12 2017-07-25 大连双迪创新科技研究院有限公司 超量氢气杀菌洗衣机
CN103938414B (zh) * 2014-04-12 2017-07-28 大连双迪创新科技研究院有限公司 洗涤助力装置
US9816194B2 (en) 2015-03-19 2017-11-14 Lam Research Corporation Control of electrolyte flow dynamics for uniform electroplating
US10014170B2 (en) 2015-05-14 2018-07-03 Lam Research Corporation Apparatus and method for electrodeposition of metals with the use of an ionically resistive ionically permeable element having spatially tailored resistivity
CN106757127A (zh) * 2015-11-23 2017-05-31 上海好旭新能源科技发展有限公司 用于电解水的无间距隔膜电解槽
US10364505B2 (en) 2016-05-24 2019-07-30 Lam Research Corporation Dynamic modulation of cross flow manifold during elecroplating
US11001934B2 (en) 2017-08-21 2021-05-11 Lam Research Corporation Methods and apparatus for flow isolation and focusing during electroplating
US10781527B2 (en) 2017-09-18 2020-09-22 Lam Research Corporation Methods and apparatus for controlling delivery of cross flowing and impinging electrolyte during electroplating
DE102018209520A1 (de) 2018-06-14 2019-12-19 Thyssenkrupp Uhde Chlorine Engineers Gmbh Elektrolysezelle
US11225724B1 (en) * 2020-07-17 2022-01-18 Key Dh Ip Inc./Ip Strategiques Dh, Inc. Integrally combined current carrier circulation chamber and frame for use in unipolar electrochemical devices
AU2021339270A1 (en) 2020-09-09 2023-03-09 Key Dh Ip Inc./Ip Strategiques Dh, Inc. Filter press end assembly and fluid management system for use in unipolar electrochemical devices
CN117735678B (zh) * 2024-02-18 2024-05-31 成都思达能环保设备有限公司 水处理方法及电解装置

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2283245A1 (fr) * 1974-08-26 1976-03-26 Hodogaya Chemical Co Ltd Ensemble d'electrode notamment pour cellule electrolytique
FR2382518A1 (fr) * 1977-03-04 1978-09-29 Ici Ltd Cellule electrolytique a membrane du type filtre-presse monopolaire
US4139448A (en) * 1978-01-03 1979-02-13 Hooker Chemicals & Plastics Corp. Separating web - electrolytic compartment frames assembly for electrolytic apparatuses
EP0047083A1 (fr) * 1980-08-29 1982-03-10 Asahi Glass Company Ltd. Procédé pour l'électrolyse d'une solution aqueuse de chlorure de métal alcalin

Family Cites Families (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3123545A (en) * 1964-03-03 Electrode for electrolytic shaping
USB230799I5 (fr) * 1958-03-18
US3657099A (en) * 1969-05-07 1972-04-18 Asahi Chemical Ind Electrolytic cell for producing adiponitrile by electrolytic hydrodimerization of acrylonitrile
EP0045148B1 (fr) * 1980-07-30 1985-05-08 Imperial Chemical Industries Plc Electrode pour utilisation dans une cellule d'électrolyse

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2283245A1 (fr) * 1974-08-26 1976-03-26 Hodogaya Chemical Co Ltd Ensemble d'electrode notamment pour cellule electrolytique
FR2382518A1 (fr) * 1977-03-04 1978-09-29 Ici Ltd Cellule electrolytique a membrane du type filtre-presse monopolaire
US4139448A (en) * 1978-01-03 1979-02-13 Hooker Chemicals & Plastics Corp. Separating web - electrolytic compartment frames assembly for electrolytic apparatuses
EP0047083A1 (fr) * 1980-08-29 1982-03-10 Asahi Glass Company Ltd. Procédé pour l'électrolyse d'une solution aqueuse de chlorure de métal alcalin

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0145259B1 (fr) * 1983-11-14 1988-10-19 Imperial Chemical Industries Plc Procédé pour l'électrolyse d'une solution aqueuse d'un chlorure de métal alcalin
EP0220846A1 (fr) * 1985-10-22 1987-05-06 Imperial Chemical Industries Plc Cellule électrolytique
US4729822A (en) * 1985-10-22 1988-03-08 Imperial Chemical Industries Plc Electrolytic cell
EP0443430A1 (fr) * 1990-02-15 1991-08-28 Asahi Glass Company Ltd. Assemblage de cellules électrolytiques monopolaires à membrane échangeuse d'ions
US5221452A (en) * 1990-02-15 1993-06-22 Asahi Glass Company Ltd. Monopolar ion exchange membrane electrolytic cell assembly
US5254233A (en) * 1990-02-15 1993-10-19 Asahi Glass Company Ltd. Monopolar ion exchange membrane electrolytic cell assembly
WO2022241518A1 (fr) * 2021-05-19 2022-11-24 Plastic Fabricators (WA) Pty Ltd t/a PFWA Cellule d'électrodialyse

Also Published As

Publication number Publication date
BR8202421A (pt) 1983-04-12
CA1203507A (fr) 1986-04-22
US4605482A (en) 1986-08-12
AU551125B2 (en) 1986-04-17
DE3277310D1 (en) 1987-10-22
EP0064608B1 (fr) 1987-09-16
AU8292082A (en) 1982-11-04

Similar Documents

Publication Publication Date Title
EP0064608B1 (fr) Cellule électrolytique du type filtre-presse
KR890003860B1 (ko) 멀티 셀 전해조
US4927509A (en) Bipolar electrolyzer
US4518113A (en) Electrolyzer and process
SK278309B6 (en) Membrane electrolytic cell
KR100645463B1 (ko) 전극 구조체
JPH0125836B2 (fr)
US4969981A (en) Cell and method of operating a liquid-gas electrochemical cell
EP0047083B1 (fr) Procédé pour l'électrolyse d'une solution aqueuse de chlorure de métal alcalin
EP0443430B1 (fr) Assemblage de cellules électrolytiques monopolaires à membrane échangeuse d'ions
US5421977A (en) Filter press electrolyzer
US4752369A (en) Electrochemical cell with improved energy efficiency
EP0139133B1 (fr) Cellule électrolytique pour l'électrolyse d'un chlorure de métal alcalin
EP0094587A1 (fr) Membrane échangeuse de cations pour l'électrolyse
US4568433A (en) Electrolytic process of an aqueous alkali metal halide solution
US4448662A (en) Solid polymer electrolyte chlor-alkali electrolytic cell
JP3229266B2 (ja) 複極式フィルタープレス型電解槽
US20040108204A1 (en) Gasket with curved configuration at peripheral edge
US5254233A (en) Monopolar ion exchange membrane electrolytic cell assembly
CA1338634C (fr) Cellule electrochimique liquide-gaz, et methode de reaction connexe
US4329218A (en) Vertical cathode pocket assembly for membrane-type electrolytic cell
JPS627885A (ja) イオン交換膜法塩化アルカリ多対電解槽
JPS6037878B2 (ja) イオン交換膜電解槽
JPS5925035B2 (ja) フイルタ−プレス式電解槽
US4342629A (en) Solid polymer electrolyte chlor-alkali process

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): BE DE FR GB IT NL SE

17P Request for examination filed

Effective date: 19830425

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Kind code of ref document: B1

Designated state(s): BE DE FR GB IT NL SE

ITF It: translation for a ep patent filed
REF Corresponds to:

Ref document number: 3277310

Country of ref document: DE

Date of ref document: 19871022

ET Fr: translation filed
PLBI Opposition filed

Free format text: ORIGINAL CODE: 0009260

26 Opposition filed

Opponent name: IMPERIAL CHEMICAL INDUSTRIES PLC

Effective date: 19880615

NLR1 Nl: opposition has been filed with the epo

Opponent name: IMPERIAL CHEMICAL INDUSTRIES PLC

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19890430

Year of fee payment: 8

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: FR

Payment date: 19900415

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19900417

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: SE

Payment date: 19900418

Year of fee payment: 9

ITTA It: last paid annual fee
PLBN Opposition rejected

Free format text: ORIGINAL CODE: 0009273

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: OPPOSITION REJECTED

27O Opposition rejected

Effective date: 19900226

NLR2 Nl: decision of opposition
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19901101

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19910403

Year of fee payment: 10

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: SE

Effective date: 19910415

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19910430

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19910430

Year of fee payment: 10

BERE Be: lapsed

Owner name: ASAHI GLASS CY LTD

Effective date: 19910430

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: FR

Effective date: 19911230

REG Reference to a national code

Ref country code: FR

Ref legal event code: ST

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19920414

GBPC Gb: european patent ceased through non-payment of renewal fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19930101

EUG Se: european patent has lapsed

Ref document number: 82103143.2

Effective date: 19911108